WO2001007365A1 - High speed manufacturing process for precipitated calcium carbonate employing sequential pressure carbonation - Google Patents
High speed manufacturing process for precipitated calcium carbonate employing sequential pressure carbonation Download PDFInfo
- Publication number
- WO2001007365A1 WO2001007365A1 PCT/US2000/019867 US0019867W WO0107365A1 WO 2001007365 A1 WO2001007365 A1 WO 2001007365A1 US 0019867 W US0019867 W US 0019867W WO 0107365 A1 WO0107365 A1 WO 0107365A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- set forth
- slurry
- calcium carbonate
- reactor
- carbon dioxide
- Prior art date
Links
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 title claims abstract description 194
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 83
- 229940088417 precipitated calcium carbonate Drugs 0.000 title claims abstract description 58
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 288
- 238000000034 method Methods 0.000 claims abstract description 233
- 238000006243 chemical reaction Methods 0.000 claims abstract description 214
- 230000008569 process Effects 0.000 claims abstract description 177
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 163
- 239000002002 slurry Substances 0.000 claims abstract description 127
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 125
- 239000000920 calcium hydroxide Substances 0.000 claims abstract description 122
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims abstract description 122
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims abstract description 121
- 229910000019 calcium carbonate Inorganic materials 0.000 claims abstract description 63
- 239000013078 crystal Substances 0.000 claims abstract description 59
- 239000000945 filler Substances 0.000 claims abstract description 35
- 239000000047 product Substances 0.000 claims abstract description 33
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 claims abstract description 29
- 229910001424 calcium ion Inorganic materials 0.000 claims abstract description 26
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims abstract description 10
- 239000002244 precipitate Substances 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 81
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 44
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 44
- 239000004571 lime Substances 0.000 claims description 44
- 230000015572 biosynthetic process Effects 0.000 claims description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 14
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 12
- 238000003860 storage Methods 0.000 claims description 11
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 9
- 239000003546 flue gas Substances 0.000 claims description 9
- 239000000292 calcium oxide Substances 0.000 claims description 8
- 238000002156 mixing Methods 0.000 claims description 8
- 238000000149 argon plasma sintering Methods 0.000 claims description 7
- 230000005587 bubbling Effects 0.000 claims description 6
- 239000002904 solvent Substances 0.000 claims description 6
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 4
- 239000000446 fuel Substances 0.000 claims description 2
- 238000001035 drying Methods 0.000 claims 4
- 239000000835 fiber Substances 0.000 claims 4
- 238000005457 optimization Methods 0.000 claims 2
- 239000004215 Carbon black (E152) Substances 0.000 claims 1
- 238000002485 combustion reaction Methods 0.000 claims 1
- 229930195733 hydrocarbon Natural products 0.000 claims 1
- 150000002430 hydrocarbons Chemical class 0.000 claims 1
- 238000005979 thermal decomposition reaction Methods 0.000 claims 1
- 238000000576 coating method Methods 0.000 abstract description 4
- 239000004615 ingredient Substances 0.000 abstract 1
- 201000003352 adrenal gland pheochromocytoma Diseases 0.000 description 132
- 235000011116 calcium hydroxide Nutrition 0.000 description 64
- 239000000123 paper Substances 0.000 description 46
- 230000001965 increasing effect Effects 0.000 description 45
- 235000010216 calcium carbonate Nutrition 0.000 description 41
- 230000006870 function Effects 0.000 description 31
- 239000002245 particle Substances 0.000 description 24
- 230000000694 effects Effects 0.000 description 17
- 230000008859 change Effects 0.000 description 15
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 13
- 238000004090 dissolution Methods 0.000 description 9
- 206010001497 Agitation Diseases 0.000 description 8
- 239000011575 calcium Substances 0.000 description 8
- 230000003247 decreasing effect Effects 0.000 description 8
- 238000002360 preparation method Methods 0.000 description 8
- 229910021532 Calcite Inorganic materials 0.000 description 7
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 7
- 229910052791 calcium Inorganic materials 0.000 description 7
- 238000013019 agitation Methods 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- 239000007864 aqueous solution Substances 0.000 description 5
- 238000009826 distribution Methods 0.000 description 5
- 238000001878 scanning electron micrograph Methods 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 239000000523 sample Substances 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 239000000498 cooling water Substances 0.000 description 3
- 230000001419 dependent effect Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 150000002500 ions Chemical class 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 238000004886 process control Methods 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- -1 Alkaline Earth Metal Carbonates Chemical class 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- 238000010420 art technique Methods 0.000 description 2
- 238000001354 calcination Methods 0.000 description 2
- 239000011248 coating agent Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000003287 optical effect Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- 230000007928 solubilization Effects 0.000 description 2
- 238000005063 solubilization Methods 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 238000004448 titration Methods 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000001154 acute effect Effects 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 229910052784 alkaline earth metal Inorganic materials 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910000020 calcium bicarbonate Inorganic materials 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 description 1
- 150000004649 carbonic acid derivatives Chemical class 0.000 description 1
- 239000008199 coating composition Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 230000001143 conditioned effect Effects 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 238000010494 dissociation reaction Methods 0.000 description 1
- 230000005593 dissociations Effects 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000010808 liquid waste Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000011087 paperboard Substances 0.000 description 1
- 239000000049 pigment Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000000135 prohibitive effect Effects 0.000 description 1
- 238000000275 quality assurance Methods 0.000 description 1
- 238000003908 quality control method Methods 0.000 description 1
- 238000005541 quenching (cooling) Methods 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
Classifications
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21H—PULP COMPOSITIONS; PREPARATION THEREOF NOT COVERED BY SUBCLASSES D21C OR D21D; IMPREGNATING OR COATING OF PAPER; TREATMENT OF FINISHED PAPER NOT COVERED BY CLASS B31 OR SUBCLASS D21G; PAPER NOT OTHERWISE PROVIDED FOR
- D21H17/00—Non-fibrous material added to the pulp, characterised by its constitution; Paper-impregnating material characterised by its constitution
- D21H17/63—Inorganic compounds
- D21H17/67—Water-insoluble compounds, e.g. fillers, pigments
- D21H17/675—Oxides, hydroxides or carbonates
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/18—Carbonates
- C01F11/181—Preparation of calcium carbonate by carbonation of aqueous solutions and characterised by control of the carbonation conditions
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2004/00—Particle morphology
- C01P2004/01—Particle morphology depicted by an image
- C01P2004/03—Particle morphology depicted by an image obtained by SEM
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2004/00—Particle morphology
- C01P2004/30—Particle morphology extending in three dimensions
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2004/00—Particle morphology
- C01P2004/30—Particle morphology extending in three dimensions
- C01P2004/39—Particle morphology extending in three dimensions parallelepiped-like
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/12—Surface area
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/60—Optical properties, e.g. expressed in CIELAB-values
Definitions
- This invention is related to a process for the production of calcium carbonate via precipitation from solubilized calcium ions and carbonate ions, and to the products of the process, and to paper products produced using the products of the process.
- the various prior art methods utilized for production of precipitated calcium carbonate in papermaking operations can be characterized in that the carbonation reaction has been carried out in an atmospheric pressure vented or open vessel. This means that the partial pressure of carbon dioxide available in the carbonation reactor has been limited based on the concentration of carbon dioxide available in an incoming gas stream.
- PCC precipitated calcium carbonate
- An average papermill may require from about 20,000 to about 100,000 tons per year of PCC.
- the production of PCC has shifted from off-site to on-site.
- One important advantage of on-site PCC production has been the saving of transportation costs.
- a primary raw material for PCC production namely carbon dioxide, is available free at many mills, as a waste product from lime kiln flue gas. Such gas normally contains from about twelve percent to about twenty five percent (12%-25%) of carbon dioxide.
- My novel manufacturing process for producing precipitated calcium carbonate can be advantageously applied to a variety of paper mill or manufacturing plant locations. This is because my process can advantageously employ low concentrations of carbon dioxide in reaction gas, such as may be found in stack gas from package boilers, or from other "low grade" carbon dioxide sources.
- My novel process is simple, easily applied to automated manufacturing process methods, and is otherwise superior to those PCC manufacturing methods heretofore used or proposed. From the foregoing, it will be apparent to the reader that one important and primary object of the present invention resides in providing an improved method for producing precipitated calcium carbonate.
- Another objective of my process, and of the apparatus for carrying out the process, is to simplify the manufacturing procedures, which importantly, simplifies and improves quality control in the manufacture of high purity precipitated calcium carbonate.
- Another objective of my process is to produce a novel, high purity, uniformly sized, calcium carbonate product via use of the process.
- Other important but more specific objects of the invention reside in the provision of an improved manufacturing process for the manufacture of precipitated calcium carbonate, as described herein, which:
- - provides a high degree of particle size uniformity, to meet optical quality requirements for use in paper manufacturing operations; - enables the production of a variety of distinct crystal morphologies, including calcite scalenohedral, calcite rhombohedral, and aragonite; enables the efficient production of small calcium carbonate crystals; enables process control to be established using reliable and batch reproducible process parameters, thus enhancing quality assurance; enables the lime slaking production rate to be matched with the precipitated calcium carbonate production rate, thus significantly increasing operating rates and thereby reducing equipment size requirements;
- My method for the production of precipitated calcium carbonate involves providing lime, either as calcium oxide or calcium hydroxide, and mixing the calcium oxide or calcium hydroxide with a solvent until a calcium hydroxide slurry is formed, with the slurry containing an undissolved solute comprising a calcium containing molecule, preferably calcium hydroxide, and a solution comprising calcium ions.
- the solvent is water
- an aqueous slurry is provided by slaking the lime.
- lime slurry can be manufactured in batches that are sized to match a desired charge volume for a carbonation reactor, or more preferably, the lime slurry can be continuously manufactured. In this way, a sequential or semi-continuous operation can be provided wherein lime slaking is matched to utilization of a slurry in a carbonation reaction batch.
- the lime slurry is charged to the carbonation reactor, which reactor is maintained at a pressure above the prevailing atmospheric pressure at the plant locale, while passing a gas stream containing carbon dioxide through the reactor.
- Carbonate ions are produced from dissociation or dissolution of the carbon dioxide in aqueous slurry, which carbonate ions react with calcium ions available from the solution carrying the lime slurry, to form a calcium carbonate precipitate.
- the lime slurry is fed to the carbonation reactor at a pH of 12 or more, and the carbonation reaction is carried out until substantially all available calcium is reacted, as indicated by reduction in pH to a pre-selected endpoint, which occurs when no further hydroxide ions become available via solvating of calcium hydroxide.
- the precipitated calcium carbonate is discharged from the carbonation reactor, and thereafter, another lime slurry charge is fed to the reactor, and the carbonation reaction is resumed.
- the lime slurry at about 200 grams per liter
- the carbonation reaction is carried out in a continuous stirred tank reactor with a high shear mechanical mixer, in order to increase the reaction rate.
- the partial pressure of carbon dioxide available for the carbonation reaction is increased by way of pressurization of the incoming gas stream to the carbonation reactor.
- This can normally be conveniently accomplished by quenching (cooling) and scrubbing an available stack gas, and then compressing the cleaned and cooled incoming gas in a gas compressor, before sending the compressed gas to the carbonation reactor.
- FIG. 1 is a graphical depiction of the reaction rate in grams of calcium hydroxide (expressed as calcium carbonate) per liter of slurry per minute, showing the increase in carbonation reaction rate as the pressure at which the carbonation reaction takes place is increased.
- Figure 2 is graphical depiction of the increase in carbonation efficiency as the pressure at which the carbonation reaction takes place is increased.
- Figure 3 is a graphical depiction of the change in surface area of precipitated calcium carbonate, showing the change as the pressure at which the carbonation reaction takes place is increased.
- Figure 4 is a graphical depiction of the change in density of a paper sheet made by utilizing the PCC produced by my novel method as a filler, with the sheet density shown as a function of the pressure at which the carbonation reaction takes place.
- Figure 5 is a graphical depiction of the change in porosity of a paper sheet made by utilizing the PCC produced by my novel method as a filler, with the sheet porosity shown as a function of the pressure at which the carbonation reaction takes place.
- Figure 6 is a graphical depiction of the change in brightness of a paper sheet made by utilizing the PCC produced by my novel method as a filler, with the sheet brightness shown as a function of the pressure at which the carbonation reaction takes place.
- Figure 7 is a graphical depiction of the change in opacity of a paper sheet made by utilizing the PCC produced by my novel method as a filler, with the sheet opacity shown as a function of the pressure at which the carbonation reaction takes place.
- Figure 8 is a graphical representation of the light scattering coefficient of the precipitated calcium carbonate produced by the present process as a function of the pressure at which the carbonation reaction takes place.
- Figure 9 is a graphical comparison of the reaction rate of the carbonation reaction as a function of the temperature at which the carbonation reaction takes place, showing the reaction rate for a gas stream containing 20 percent carbon dioxide, at 0 psig (atmospheric pressure) and at 30 psig.
- Figure 10 is a graphical comparison of the carbon dioxide usage efficiency as function of the temperature at which the carbonation reaction is carried out, showing the efficiency for a gas stream containing 20 percent carbon dioxide, at 0 psig (atmospheric pressure), and at 30 psig.
- Figure 11 is a graphical representation of the surface area (shown as Blaine) of PCC as a function of the temperature at which the carbonation reaction is carried out, showing the PCC surface area for a gas stream containing 20 percent carbon dioxide at
- Figure 12 is a graphical depiction of the change in density of a paper sheet made by utilizing the PCC produced by my novel method as a filler, with the sheet density shown as a function of the temperature at which the carbonation reaction takes place.
- Figure 13 is a graphical depiction of the change in porosity of a paper sheet made by utilizing the PCC produced by my novel method as a filler, with the sheet porosity shown as a function of the temperature at which the carbonation reaction takes place.
- Figure 14 is a graphical depiction of the change in brightness of a paper sheet made by utilizing the PCC produced by my novel method as a filler, with the sheet brightness shown as a function of the temperature at which the carbonation reaction takes place.
- Figure 15 is a graphical depiction of the change in opacity of a paper sheet made by utilizing the PCC produced by my novel method as a filler, with the sheet opacity shown as a function of the temperature at which the carbonation reaction takes place.
- Figure 16 is a graphical representation of the light scattering coefficient of the precipitated calcium carbonate produced by the present process as a function of the temperature at which the carbonation reaction takes place.
- Figure 17 is a graphical representation of the reaction rate of the carbonation reaction as a function of the percentage of carbon dioxide a gas stream provided to the carbonation reactor, showing the efficiency for a gas stream at 0 psig (atmospheric pressure), and clearly showing the increased reaction rate when using my novel process at 30 psig.
- Figure 18 is a graphical representation of the carbonation reaction efficiency as a function of the percentage of carbon dioxide in a gas stream provided to the carbonation reactor, showing the efficiency for a gas stream at 0 psig (atmospheric pressure), and clearly showing the increased efficiency when using my novel process at 30 psig.
- Figure 19 is a graphical representation of the surface area of precipitated calcium carbonate (as indicated by Blaine) a function of the percentage of carbon dioxide in a gas stream provided to the carbonation reactor, showing the efficiency for a gas stream at 0 psig (atmospheric pressure), and showing the increased surface area when using my novel process at 30 psig, for low (5% by volume) to moderate (20%> by volume) carbon dioxide concentrations.
- Figure 20 is a graphical depiction of the change in density of a paper sheet made with precipitated calcium carbonate, with the sheet density shown as a function of the concentration of carbon dioxide in the carbonation reactor incoming gas stream, for 0 psig (atmospheric pressure), and showing the density when using my novel process at 30 psig.
- Figure 21 is a graphical depiction of the change in porosity of a paper sheet made by utilizing precipitated calcium carbonate, with the sheet porosity shown as a function of the concentration of carbon dioxide in the carbonation reactor incoming gas stream, for 0 psig (atmospheric pressure), and showing the porosity when using my novel process at 30 psig.
- Figure 22 is a graphical depiction of the change in brightness of a paper sheet made by utilizing PCC as a filler, with the sheet brightness shown as a function of the concentration of carbon dioxide in the carbonation reactor incoming gas stream, for 0 psig (atmospheric pressure), and showing the brightness when using my novel process at 30 psig for the production of PCC.
- Figure 23 is a graphical depiction of the change in opacity of a paper sheet made utilizing PCC as a filler, with the sheet opacity shown as a function concentration of carbon dioxide in the carbonation reactor incoming gas stream, for 0 psig (atmospheric pressure), and showing the opacity when using my novel process at 30 psig for the production of PCC.
- Figure 24 is a graphical representation of the light scattering coefficient of PCC as a function concentration of carbon dioxide in the carbonation reactor incoming gas stream, for 0 psig (atmospheric pressure), and showing the light scattering coefficient when using my novel process at 30 psig for the production of PCC.
- Figure 25 is a graphical representation of the reaction rate of the carbonation reaction, in terms of the grams per liter per minute of calcium hydroxide converted, as a function of the concentration of calcium hydroxide in the lime slurry (expressed as grams of calcium hydroxide as calcium carbonate, per liter of slurry), for a reaction according to my invention, carried out at 30 psig and 100°F using a gas stream to the carbonation reaction which contains 20% carbon dioxide by volume.
- Figure 26 is a graphical representation of the carbon dioxide efficiency, in the carbonation reaction as a function of the concentration of calcium hydroxide in the lime slurry (expressed as grams of calcium hydroxide as calcium carbonate, per liter of slurry), for a reaction according to my invention, carried out at 30 psig and 100°F using a gas stream which contains 20% carbon dioxide by volume upon entry to the carbonation reactor.
- Figure 27 is a graphical representation of the surface area (Blaine) of PCC produced by my process as a function of the concentration of calcium hydroxide in the lime slurry (expressed as grams of calcium hydroxide as calcium carbonate, per liter of slurry), for a reaction according to my invention carried out at 30 psig and 100°F using a gas stream to the carbonation reaction which contains 20% carbon dioxide by volume.
- Figure 28 is a graphical representation of the reaction rate of the carbonation reaction as a function of the speed of the agitator used to stir the lime slurry in the reactor, for a reaction carried out at 30 psig and 100°F using a gas stream entering the carbonation reactor which contains 20% carbon dioxide by volume.
- Figure 29 is a graphical representation of the carbon dioxide utilization efficiency as a function of the speed of the agitator used to stir the lime slurry in the reactor, for a reaction carried out at 30 psig and 100°F using a gas stream entering the carbonation reactor which contains 20 percent carbon dioxide by volume.
- Figure 30 is a graphical representation of the surface area (Blaine) of the PCC made in my novel process, expressed as a function of the speed of the agitator used to stir the lime slurry in the reactor, for a reaction carried out at 30 psig and 100°F using a gas stream entering the carbonation reactor which contains 20%) carbon dioxide by volume.
- Figure 31 is a photograph of the sclenohedral crystals of precipitated calcium carbonate obtained in the process of the present invention; the photographs were taken with a scanning electromicroscope (SEM).
- Figure 32 is a photograph of the rhombohedral crystals of precipitated calcium carbonate obtained in the process of the present invention, where the crystals have an aspect ratio of approximately 1 : 1 ; the photographs were taken with a scanning electromicroscope (SEM).
- Figure 33 is a photograph of the rhombohedral crystals of precipitated calcium carbonate obtained in the process of the present invention, where the crystals have an aspect ration of approximately 1 :1.5; the photographs were taken with a scanning electromicroscope (SEM).
- Figure 34 is a photograph of the stacked rhombohedral crystals of precipitated calcium carbonate obtained in the process of the present invention; the photographs were taken with a scanning electromicroscope (SEM).
- Figure 35 is a photograph of the aragonite crystals of precipitated calcium carbonate obtained in the process of the present invention; the photographs were taken with a scanning electromicroscope (SEM).
- Figure 36 is a process flow diagram showing one convenient arrangement for lime slaking, to prepare a calcium hydroxide slurry for feed to a pressurized carbonation reactor, in order to carry out the process of the present invention.
- Figure 37 is a process flow diagram showing one convenient configuration for gas compression, or alternate carbon dioxide preparation, for feed of pressurized carbon dioxide to a pressurized reactor, in order to carry out the process of the present invention.
- Figure 38 is a process flow diagram showing one convenient arrangement for reaction of lime slurry with carbon dioxide under pressurized conditions, and for final preparation of the product produced in the carbonation reactor.
- a novel process for producing precipitated calcium carbonate is provided which enables the efficient use of "free” carbon dioxide found in flue gas, and more particularly, from flue gas containing relatively low concentrations of carbon dioxide.
- This process is capable of providing a variety of PCC morphologies, and the use of such
- PCC produced by this process has some unique properties for use as a filler in papermaking operations. This in turn results in some unusual and beneficial paper properties for the superior paper products made with the PCC provided according to the inventive process disclosed herein.
- the precipitated carbonates that can be manufactured by this process include distinct crystal morphologies including calcite scalenohedral, calcite rhombohedral of various aspect ratios, and aragonite.
- the final carbonation reaction is an equilibrium reaction. Therefore, as the
- the calcium hydroxide takes place from the lime slurry to increase the concentration of
- the carbonation reaction is accompanied by the evolution of heat (i.e, it is an exothermic reaction).
- the pH of the lime slurry decreases during the course of the reaction of a batch of lime with carbon dioxide, and such pH changes from approximately 12.4 to the equilibrium pH of 8, plus or minus about 1 pH unit.
- the rate of dissolution of Ca(OH) 2 is a function of the temperature and of the pressure at which the dissolution takes place. This is important since the controlling reaction in the overall calcium carbonate production process is the dissolution of the available calcium hydroxide, which is only sparingly soluble in aqueous solution, and which is inversely dependent upon temperature in aqueous solution.
- the conventional industrial process for production of precipitated calcium carbonate is performed by providing a slurry of approximately 200g/L of calcium hydroxide in an atmospheric reactor, and bubbling a gas stream containing carbon dioxide at about 15-20% by volume into the reactor.
- reaction rates in the range of from about 0.5 grams per liter of slurry per minute to about 1.5 grams per liter of slurry per minute are commonly seen.
- the time required to complete the reaction in the carbonation reactor is approximately 200minutes. That relatively slow overall reaction rate results in a requirement for large carbonation reactors ( reactors in the 18,000 to 20,000 gallon range are common), with the associated high capital costs.
- Calcium oxide (lime) 54 is normally delivered from a rail car (not shown) via hopper or conveyor or other transport device such as pneumatic tube powered by blower to an incoming lime storage silo 56.
- a feeder sends stored lime via conveyor to a slaker tank 62 which is stirred by high sheer mixing agitator 64.
- Slaking water is added to slaker tank 62 via line 66 from mill water storage tank 68.
- Storage tank 68 can be fed with water and steam to provide a desired water temperature in storage tank 68.
- Slaked lime is pumped via pump 69 to screen 70 to remove oversize materials.
- Grit 72 is captured and sent via screw conveyor 74 to grit bin 75.
- the stirred slaked lime slurry is dropped into a mixer 80 stirred surge tank 84 and then pumped 86 via heat exchanger 88 to a storage tank 90 which is stirred by agitator 92.
- the volume of slurry stored in storage tank 90 matches the charge required by carbonation reactor 100 (see FIG. 38), so that once a batch of slurry is sent from tank 90 to carbonation reactor 100, the storage tank 90 can be refilled with another batch of slurry.
- the lime slurry discharged from tank 90 via pump 101 can be cooled via chiller 102, or other convenient heat exchange apparatus or process in order to increase the solubility of calcium in aqueous liquid in the carbonation reactor 100.
- Any convenient source of carbon dioxide can be utilized in my novel process, ranging from fresh carbon dioxide provided from storage tanks 103, or more commonly, flue gas 104 which is sent to quencher 106 for cooling by a cooling water stream 108.
- the quenched gases flow via line 110 to compressor 112 which increases the pressure of the gas stream, thus increasing the partial pressure of carbon dioxide supplied to the carbonation reactor 100.
- the compressed gas stream 114 is sent to a heat exchanger
- the lime slurry at a preselected temperature is sent from storage tank 90 to carbonation reactor 100 via line 132. During the reaction of a batch of slurry in reactor
- the pH of the liquid in the carbonation reactor 100 is measured by pH probe 134 or by other suitable method or means, until the pH falls and ultimately reaches a desired endpoint that indicates that available calcium has been consumed.
- agitator 136 maintains high shear agitation in reactor 100. Agitator 136 therefore has a high tip speed, ranging from about 260 feet per minute up to about 780 feet per minute, depending upon the design configuration.
- the present invention involves carrying out the carbonation reaction between CO 2 and Ca(OH) 2 under pressure in a carbonation reactor 100 which is a pressure vessel.
- This novel process involves bubbling CO 2 into the Ca(OH) 2 slurry in reactor 100 where the pressure can range from above atmospheric pressure to as much as about
- the pressure in the reactor 100 is maintained at up to about 30 psig, and more preferably, the pressure in the reactor is maintained in the range from about 15 psig to about 30 psig.
- Inert gas and any residual carbon dioxide not utilized (such loss is kept to an absolute minimum) in reactor 100 is routed via vent line 138 to the atmosphere.
- the reaction rate can be increased from the rate of about 1.0 grams of calcium hydroxide per liter of slurry per minute to up to 10 grams of calcium hydroxide per liter of slurry per minute.
- a production rate increase of as much as 10 fold can be achieved by utilizing my novel process.
- This dramatic increase in reaction rate results in a decrease in carbonation time from the prior art range of 180 to 200 minutes per batch (when conducted at atmospheric pressure conditions) to as low as 30 to 40 minutes per batch (when conducted under pressurized conditions in carbonation reactor 100).
- the carbonation reactor can be sized less than 200 gallons capacity per ton per day of PCC output, and more preferably, less than 100 gallons capacity per ton per day, and most preferably, less than 50 gallons per ton per day of PCC output.
- key process parameters such as reaction temperature, carbon dioxide partial pressure, flow rate of carbon dioxide, lime slurry concentration in the carbonation reactor, agitator speed in the carbonation reactor, can be more effectively employed, in order to (a) increase the rate of carbonation reaction, (b) increase the carbonation efficiency, i.e., carbon dioxide utilization, and (c) to produce CaCO 3 particles of different morphology, shape, size, and size distribution.
- the precipitated calcium carbonate produced in carbonation reactor 100 is discharged, preferably a PCC batch tank 182 which is stirred by agitator 184. Each PCC batch is then discharged via pump 186 to final screens 188, where any remaining oversize material is removed and sent via chute 190 to conveyor 72 and ultimately to grit bin 74.
- the produced PCC is received in tank 200.
- line 200 the precipitated calcium carbonate produced in carbonation reactor 100 is discharged, preferably a PCC batch tank 182 which is stirred by agitator 184.
- Each PCC batch is then discharged via pump 186 to final screens 188, where any remaining oversize material is removed and sent via chute 190 to conveyor 72 and ultimately to grit bin 74.
- the produced PCC is received in tank 200.
- Tank 200 is preferably, but need not be, atmospheric.
- the product PCC is stored in tank 202, and mixed with agitator 204, before being sent via pump 206 to the papermill.
- the higher reaction pressure evidently also increases the solubilization of Ca(OH) 2 slurry into calcium ions (Ca ++ ). This results in a higher reaction rate, due to increased calcium ion availability, which in turn reduces the reaction time of calcium carbonate formation.
- My novel pressure carbonation process for the production of PCC can also produce a wide variety of crystal habits, including like calcite, rhombohedral, and aragonite in different sizes, shapes, and aspect ratios.
- the PCC provided by the instant invention produces crystals which improve key paper properties, including porosity, density, brightness, and opacity.
- temperature, after slaking, is normally in the range from about 150°F to about 160°F.
- the resulting calcium hydroxide slurry is screened, preferably through a
- the screened Ca(OH) 2 slurry is then transferred into a reaction vessel of 1.6L total capacity.
- the reactor is capable of being heating with outside jacketed heaters.
- the system can be sealed and operated at super atmospheric pressures (i.e. at pressures greater than atmosphere).
- the reactor is also fitted with a cooling coil to maintain isothermal temperature, when desired necessary.
- the agitator impeller used is a Rustin 200.
- the agitator / impeller is connected to a magnetic, variable speed, drive.
- the particular vessel is also fitted with a dip or a sample tube.
- the primary purpose of the dip tube is to obtain samples of Ca(OH) 2 / CaCO 3 slurry periodically and to follow the conversion of calcium hydroxide to calcium carbonate by measuring pH and /or by titration.
- the experimental reactor is also connected to a temperature controller via a transducer
- the reaction conditions were varied to meet the specific requirement of reaction rate, particle size, shape and mo ⁇ hologies.
- the Ca(OH) 2 concentration used ranged from 50grams per liter of slurry (90%) CaO) to a high of about 300grams per liter of slurry.
- the preferred concentration was about 250grams of calcium hydroxide per liter of slurry.
- carbonation temperature was varied from 60 °F to 130 °F. In generally, the selected
- sclenohedral PCC was manufactured in the range of 90 °F to
- the carbon dioxide concentration was also varied from a low of 5.0%> CO 2 / 95% N 2 by volume to a high of 100% CO 2 / 0% N 2 by volume.
- the preferred CO 2 concentration fraction was 20%> CO 2 with the remainder 80%> N 2 , by volume.
- Another important variable is the flow rate of the carbon dioxide through the carbonation reactor.
- the flow of carbon dioxide was varied from a conventional flow rate of 0.5 L / min to 4.0 L / min.
- the preferred flow rate was 1.5 liters per minute for the above noted size reactor.
- the rate of agitation of the impeller speed is important, in order to maintain high rates of mass transfer of CO 2 (gas) into dissolved CO 2 (aqueous), i.e, the rate of carbonic acid formation.
- the agitator speed was varied from 500 ⁇ m to 1500 ⁇ m. The preferred ⁇ m was 1470.
- operating the carbonation reaction under isothermal conditions resulted in unique PCC products.
- the carbonation reaction is an exothermic reaction, the progress of the reaction was accompanied by an observed increase in temperature.
- the reaction kinetics were determined using temperature to indicate the endpoint of the carbonation reaction. As the conversion of Ca(OH) 2 into CaCO 3 was completed, the temperature reached a maximum, and then dropped.
- a temperature probe controller connected to the reaction vessel was used to follow the rise and fall of the reaction temperature.
- the temperature profile was used to indicate the reaction end point.
- the chemical analysis of the final product, and pH, confirmed the finding of the carbonation reaction end point. If the pH drifts higher, then the carbon dioxide can be applied sequentially until stable pH is achieved.
- the calcium carbonate formed under the novel pressure carbonation technique was filtered through a Whatman #212 filter paper using a vacuum pump, and was washed to remove impurities. One portion of the sample was dried, and the other portion was reslurried for end use in performance testing via preparation of paper handsheets.
- Example 1 The Effect of Pressure in a Pressure Carbonation System on Reaction Rate. Carbonation Efficiency, and Surface Area
- the carbonation reaction pressure was raised from 0 psig (as done with a conventional open tank PCC system) to 70 psig. The reaction
- the resulting experimental data is given in Table IB.
- the resulting reaction rate at 0 psig was 4.6 grams per liter of slurry per minute. In the pressure carbonation system operating at 70 psig, it was 6.1 grams per liter per minute. The increase in reaction rate was approximately 33%>.
- the surface area (Blaine) of the PCC produced by the process increased from 31,400 cm 2 /gram at 0 psig, to a maximum of 40,200 cm 2 /g at 50 psig, and then decreased slightly to 35,500 cm 2 /g at 70 psig. See Figures 1, 2, and 3.
- the PCC batches prepared in Example 1 were then used to prepare paper handsheets. Some of the key paper properties, including sheet density, sheet porosity, sheet brightness, and sheet opacity, were then measured in each of the handsheets which were formed.
- the data from tests on handsheets is provided in Table IB below.
- a graphical representation of the data is also provided in Figures 4 through 9 below. It is important to note some of the key characteristics of paper made from PCC under different carbonation pressures.
- the sheet density of paper handsheets containing PCC produced under increasing pressure is shown in Figure 4.
- the sheet porosity of paper handsheets containing PCC produced under increasing pressure is shown in Figure 5.
- the sheet brightness of paper handsheets containing PCC produced under pressure decreased as pressures increased up to about 30 psig.
- the sheet brightness increases as the reaction pressure was increased from 30 psig to 70 psig.
- the sheet opacity of paper handsheets increased as the pressure of the carbonation reaction producing the PCC increased.
- the scattering coefficient of handsheets produced using PCC manufactured under pressure carbonation proved higher than the scattering coefficient of PCC produced at 0 psig as in a conventional, open system.
- Example 2 The Effect of Temperature in a "Pressure Carbonation" System As in example 1 , the slaked lime was placed into a reactor at a slurry concentration of 250 grams of calcium hydroxide grams per liter. The starting
- the carbonation reaction conditions and the experimental data resulting is shown in Table 2 A and in Table 2B.
- the reaction rates at varying temperature, for a prior art atmospheric system (0 psig) are shown in Figure 9.
- the corresponding reaction rates for my "pressurized carbonation" system operating at 30 psig are also shown in Figure 9.
- the graphs indicate that in the pressurized carbonation process, the reaction rates steadily increased as a function of temperature.
- a pressurized carbonation system provided a higher reaction rate throughout the whole range of operating temperature.
- PCC as measured by Blaine for both the pressurized and non-pressurized systems at different temperatures, is provided in Figure 11.
- the surface area of the product decreased as the reaction temperature was increased.
- the surface area of calcium carbonate decreased from approximately 44,000 cm 2 /g to a coarse PCC of 22,000 cm 2 /g.
- the controllability of surface area via temperature was more linear under pressurized carbonation conditions, at least at the 30 psig condition which was tested.
- Table 2A The Effect of Temperature on Reaction Rate, Carbonation Efficiency, and Surface Area in a Non-Pressurized System.
- Example 3 The effect of %>CO, Concentration on Reaction Rate. Carbonation Efficiency, and Surface Area
- concentration of CO 2 was varied from 5.0% CO c / 95%o N 2 to 100% CO 2 / 0% N 2 , by volume.
- Other reaction conditions were kept constant at the following levels:
- Table 3A The Effect of CO 2 Concentration on Reaction Rate, Carbonation Efficiency, and Surface Area in a Pressurized System.
- Table 3B Comparative Example -The Effect of CO 2 Concentration on Reaction Rate, Carbonation Efficiency, and Surface Area in a Non-Pressurized System.
- the PCC produced under pressure carbonation conditions at different carbon dioxide concentrations was used to make paper handsheets.
- the quality data of key paper properties is set forth in Tables 3C, for handsheets made with PCC manufactured under pressure carbonation conditions, and in Table 3D, for handsheets made with PCC manufactured under atmospheric conditions.
- the graphical representations of the data are shown in Figures 20 through 24.
- the key characteristics of the paper handsheets as a function of carbon dioxide concentration are given below.
- Figure 20 in paper produced using PCC manufactured under pressure carbonation conditions, the sheet density is shown to increase with increasing carbon dioxide concentration.
- the Gurley sheet porosity increased over paper produced using PCC manufactured under atmospheric conditions.
- the higher Gurley sheet porosity seen in handsheets made from PCC manufactured under pressure carbonation conditions means that tighter sheets were made possible by utilizing PCC manufactured under pressure.
- Example 4 The Effect of Calcium Hydroxide Concentration on Reaction Rate. Carbonation Efficiencv.and Surface Area of PCC
- concentration of calcium hydroxide was varied from a low of 35 grams per liter to a high of 308 grams per liter, measured as calcium carbonate (24 grams per liter of calcium hydroxide to about 228 grams per liter calcium hydroxide, as ion).
- the constant reaction conditions were as follows:
- reaction rate and the carbon dioxide utilization efficiency decreased as the concentration of Ca(OH) 2 increased to about 125 grams per liter of calcium hydroxide. However, beyond 150 grams per liter, the reaction rate and the carbon dioxide utilization efficiency increased, reaching a maximum at, or slightly less than, about ⁇ 300 grams per liter of Ca(OH) 2 .
- Table 4 The Effect of Calcium Hydroxide Concentration on Reaction Rate, Carbonation Efficiency, and Surface Area.
- the slaked lime was placed in a pressurized reactor vessel.
- the agitation in the reaction vessel was successively increased from 500 RPM to about 1800 RPM on the agitator.
- the other reaction conditions were kept constant at the following levels:
- Carbonation Pressure 30 psig
- the reaction rate was measured by titration of the lime slurry at regular intervals.
- the experimental data is given in Table 5.
- the reaction rate of carbonation increased three fold from about 2.0 grams per liter per minute of calcium hydroxide consumption to about 6.0 grams per liter per minute of calcium hydroxide consumption.
- the carbonation efficiency increased from a low of 35.0% > to a high of 99.6%>, as indicated in Figure 29.
- the particle surface area of PCC manufactured under pressure carbonation conditions of 30 psig increased from a low of 27,900 cm 2 /g as measured by Blaine, to about to 43,400 cm 2 /g.
- Table 5 The Effect of Agitation on Reaction Rate, Carbonation Efficiency, and Surface Area.
- a slaked lime slurry having a concentration of 246 grams per liter of slurry was placed in a pressurized reaction vessel.
- a gas mixture of 20% carbon dioxide/ 80%) nitrogen was bubbled through the reactor.
- the initial carbonation reaction temperature was at 100°F.
- the pressure in the carbonation reaction vessel was maintained at 30 psig.
- a slaked lime slurry having a concentration of 87 grams per liter of calcium hydroxide slurry (expressed as calcium carbonate) was placed in a pressurized reaction vessel.
- a gas mixture of 20%> carbon dioxide/ 80%> nitrogen was bubbled through the reactor.
- the initial carbonation reaction temperature was at 68°F.
- the increase of reaction temperature was limited to 4.0°F by circulating cooling water through the reactor.
- the pressure in the reaction vessel during pressure carbonation was maintained at 20 psig.
- the PCC manufactured under such pressurized carbonation conditions had the following characteristics:
- PCC with various aspect ratios can easily and reliably be produced using my pressurized carbonation process.
- Aspect ratio is the ratio of crystal breadth to crystal length, and is considered a semi-qualitative number.
- a slaked lime slurry having a concentration of 116 grams per liter of calcium hydroxide slurry (expressed as calcium carbonate) was placed in a pressurized reaction vessel.
- a gas mixture of 20%» carbon dioxide/ 80%> nitrogen was bubbled through the reactor.
- the initial carbonation reaction temperature was at 50°F.
- the reaction was carried out under isothermal conditions, and thus, heat generated by the exothermic nature of the reaction was removed with circulating cooling water to maintain the reactor temperature.
- the pressure in the reaction vessel during pressure carbonation was maintained at 30 psig.
- the PCC manufactured under such pressurized carbonation conditions had the following characteristics:
- a unique "stacked" PCC crystal structure can be reliably produced using my pressurized carbonation process.
- a slaked lime slurry having a concentration of 32 grams per liter of calcium hydroxide slurry (expressed as calcium carbonate) was placed in a pressurized reaction vessel.
- a gas mixture of 25%> carbon dioxide/ 75% nitrogen was bubbled through the reactor.
- the initial carbonation reaction temperature was at 73°F.
- the carbonation pressure was maintained at 70 psig.
- aragonite crystal habit PCC crystal structure can be reliably produced using my pressurized carbonation process.
- a slaked lime slurry having a concentration of 229 grams per liter of calcium hydroxide slurry (expressed as calcium carbonate) was placed in a pressurized reaction vessel.
- a gas mixture of 25% carbon dioxide/ 75% nitrogen by volume was bubbled through the reactor.
- the initial carbonation reaction temperature was at 120°F.
- the carbonation pressure was maintained at 70 psig.
- the reaction yielded a PCC with the following characteristics: Surface Area 23,500 cm 2 /gram (measured by Blaine)
- the pressure carbonation for production of PCC process as described herein can be used with any convenient source of carbon dioxide, since the pressurization of the reactor advantageously increases the partial pressure of carbon dioxide to an extent that it can be economically exploited. It is to be appreciated that my process for the production of precipitated calcium carbonate is an appreciable improvement in the state of the art for on-site production of calcium carbonate. My novel process treats the manufacture of calcium carbonate in a manufacturing environment from a new perspective, to provide significantly improved production rates.
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP00950496A EP1230160A4 (en) | 1999-07-21 | 2000-07-21 | High speed manufacturing process for precipitated calcium carbonate employing sequential pressure carbonation |
CA002416080A CA2416080C (en) | 1999-07-21 | 2000-07-21 | High speed manufacturing process for precipitated calcium carbonate employing sequential pressure carbonation |
AU63595/00A AU6359500A (en) | 1999-07-21 | 2000-07-21 | High speed manufacturing process for precipitated calcium carbonate employing sequential pressure carbonation |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US09/358,759 | 1999-07-21 | ||
US09/358,759 US6251356B1 (en) | 1999-07-21 | 1999-07-21 | High speed manufacturing process for precipitated calcium carbonate employing sequential perssure carbonation |
Publications (2)
Publication Number | Publication Date |
---|---|
WO2001007365A1 true WO2001007365A1 (en) | 2001-02-01 |
WO2001007365A9 WO2001007365A9 (en) | 2002-07-25 |
Family
ID=23410922
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/US2000/019867 WO2001007365A1 (en) | 1999-07-21 | 2000-07-21 | High speed manufacturing process for precipitated calcium carbonate employing sequential pressure carbonation |
Country Status (5)
Country | Link |
---|---|
US (2) | US6251356B1 (en) |
EP (1) | EP1230160A4 (en) |
AU (1) | AU6359500A (en) |
CA (1) | CA2416080C (en) |
WO (1) | WO2001007365A1 (en) |
Cited By (28)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN100389068C (en) * | 2004-09-24 | 2008-05-21 | 曲玉珠 | Preparation of light calcium carbonate by calcite |
EP2157136A1 (en) | 2008-08-13 | 2010-02-24 | Omya Development Ag | Process to prepare precipitated calcium carbonate implementing low charge acrylate a/o maleinate-containing polymer |
US7735274B2 (en) | 2007-05-24 | 2010-06-15 | Calera Corporation | Hydraulic cements comprising carbonate compound compositions |
US7744761B2 (en) | 2007-06-28 | 2010-06-29 | Calera Corporation | Desalination methods and systems that include carbonate compound precipitation |
US7749476B2 (en) | 2007-12-28 | 2010-07-06 | Calera Corporation | Production of carbonate-containing compositions from material comprising metal silicates |
US7754169B2 (en) | 2007-12-28 | 2010-07-13 | Calera Corporation | Methods and systems for utilizing waste sources of metal oxides |
US7753618B2 (en) | 2007-06-28 | 2010-07-13 | Calera Corporation | Rocks and aggregate, and methods of making and using the same |
US7771684B2 (en) | 2008-09-30 | 2010-08-10 | Calera Corporation | CO2-sequestering formed building materials |
US7790012B2 (en) | 2008-12-23 | 2010-09-07 | Calera Corporation | Low energy electrochemical hydroxide system and method |
US7815880B2 (en) | 2008-09-30 | 2010-10-19 | Calera Corporation | Reduced-carbon footprint concrete compositions |
US7829053B2 (en) | 2008-10-31 | 2010-11-09 | Calera Corporation | Non-cementitious compositions comprising CO2 sequestering additives |
US7875163B2 (en) | 2008-07-16 | 2011-01-25 | Calera Corporation | Low energy 4-cell electrochemical system with carbon dioxide gas |
US7887694B2 (en) | 2007-12-28 | 2011-02-15 | Calera Corporation | Methods of sequestering CO2 |
US7939336B2 (en) | 2008-09-30 | 2011-05-10 | Calera Corporation | Compositions and methods using substances containing carbon |
US7966250B2 (en) | 2008-09-11 | 2011-06-21 | Calera Corporation | CO2 commodity trading system and method |
US7993500B2 (en) | 2008-07-16 | 2011-08-09 | Calera Corporation | Gas diffusion anode and CO2 cathode electrolyte system |
US7993511B2 (en) | 2009-07-15 | 2011-08-09 | Calera Corporation | Electrochemical production of an alkaline solution using CO2 |
US8137444B2 (en) | 2009-03-10 | 2012-03-20 | Calera Corporation | Systems and methods for processing CO2 |
CN102423608A (en) * | 2011-10-28 | 2012-04-25 | 长沙理工大学 | Desulfurizer prepared by causticized white mud and method thereof for flue gas desulphurization |
US8357270B2 (en) | 2008-07-16 | 2013-01-22 | Calera Corporation | CO2 utilization in electrochemical systems |
US8491858B2 (en) | 2009-03-02 | 2013-07-23 | Calera Corporation | Gas stream multi-pollutants control systems and methods |
WO2014016469A1 (en) * | 2012-07-27 | 2014-01-30 | Upm-Kymmene Corporation | A method and a system for preventing calender blackening |
US8834688B2 (en) | 2009-02-10 | 2014-09-16 | Calera Corporation | Low-voltage alkaline production using hydrogen and electrocatalytic electrodes |
US8869477B2 (en) | 2008-09-30 | 2014-10-28 | Calera Corporation | Formed building materials |
RU2533143C1 (en) * | 2013-03-26 | 2014-11-20 | Геннадий Георгиевич Волокитин | Method of obtaining ultradispersive powders of carbonates |
US9133581B2 (en) | 2008-10-31 | 2015-09-15 | Calera Corporation | Non-cementitious compositions comprising vaterite and methods thereof |
US9260314B2 (en) | 2007-12-28 | 2016-02-16 | Calera Corporation | Methods and systems for utilizing waste sources of metal oxides |
EP2268863B1 (en) | 2008-03-07 | 2019-12-18 | FP-Pigments Oy | A pigment particle composition, its method of manufacture and its use |
Families Citing this family (41)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7048900B2 (en) * | 2001-01-31 | 2006-05-23 | G.R. International, Inc. | Method and apparatus for production of precipitated calcium carbonate and silicate compounds in common process equipment |
FR2821095B1 (en) * | 2001-02-16 | 2003-04-11 | Arjo Wiggins Sa | PROCESS FOR OBTAINING A PAPER SHEET CONTAINING CALCITE |
US6413365B1 (en) * | 2001-07-11 | 2002-07-02 | Voith Paper Patent Gmbh | Method of loading a fiber suspension with calcium carbonate |
EP1501982A1 (en) * | 2002-05-03 | 2005-02-02 | Imerys Minerals Limited | Paper coating pigments |
DE60336000D1 (en) * | 2002-09-20 | 2011-03-24 | Panasonic Corp | PROCESS FOR PRODUCING NANOTEILES |
US7056419B2 (en) * | 2002-09-30 | 2006-06-06 | American Air Liquide, Inc. | Methods for modifying electrical properties of papermaking compositions using carbon dioxide |
US7132090B2 (en) * | 2003-05-02 | 2006-11-07 | General Motors Corporation | Sequestration of carbon dioxide |
US20050089466A1 (en) * | 2003-10-27 | 2005-04-28 | Degenova Mark G. | Methods and apparatus for producing precipitated calcium carbonate |
SE528693C2 (en) * | 2004-07-02 | 2007-01-23 | Chematur Eng Ab | Process and system for producing precipitated calcium carbonate |
CN101031686A (en) * | 2004-07-14 | 2007-09-05 | 国际纸业公司 | Method to manufacture paper |
DE102004045089A1 (en) * | 2004-09-17 | 2006-03-23 | Voith Paper Patent Gmbh | Method and device for loading a pulp suspension |
EP1712597A1 (en) | 2005-04-11 | 2006-10-18 | Omya Development AG | Process for preparing precipitated calcium carbonate pigment, especially for use in inkjet printing pater coatings and precipitated calcium carbonate |
EP1712523A1 (en) * | 2005-04-11 | 2006-10-18 | Omya Development AG | Precipitated calcium carbonate pigment, especially for use in inkjet printing paper coatings |
FR2885900B1 (en) * | 2005-05-20 | 2009-02-13 | Omya Development Ag | MINERAL MATERIALS CONTAINING CARBONATE WITH REDUCED FOSSIL FUEL CELL CARBONIC GAS EMISSION AT THE TIME OF THEIR DECOMPOSITIONS AND THEIR SYNTHESIS PROCESS AND USES THEREOF. |
FR2894846B1 (en) * | 2005-12-20 | 2008-02-01 | Coatex Sas | USE OF DISPERSANTS FOR CONCENTRATING MINERALS IN WATER, DISPERSIONS OBTAINED AND USES THEREOF. |
US20080053337A1 (en) * | 2006-09-01 | 2008-03-06 | Joseph Andrew Sohara | Precipitated calcium carbonate from kraft pulp lime mud for use in filled and coated paper |
SI2011766T1 (en) * | 2007-06-15 | 2009-08-31 | Omya Development Ag | Surface-reacted calcium carbonate in combination with hydrophobic adsorbent for water treatment |
WO2010074687A1 (en) * | 2008-12-23 | 2010-07-01 | Calera Corporation | Low-energy electrochemical proton transfer system and method |
DE602007009124D1 (en) * | 2007-12-12 | 2010-10-21 | Omya Development Ag | Process for the preparation of surface-reactive precipitated calcium carbonate |
US20100144521A1 (en) * | 2008-05-29 | 2010-06-10 | Brent Constantz | Rocks and Aggregate, and Methods of Making and Using the Same |
WO2010068924A1 (en) * | 2008-12-11 | 2010-06-17 | Calera Corporation | Processing co2 utilizing a recirculating solution |
US20100258035A1 (en) * | 2008-12-24 | 2010-10-14 | Brent Constantz | Compositions and methods using substances containing carbon |
US20110091366A1 (en) * | 2008-12-24 | 2011-04-21 | Treavor Kendall | Neutralization of acid and production of carbonate-containing compositions |
EP2240629A4 (en) * | 2009-01-28 | 2013-04-24 | Calera Corp | Low-energy electrochemical bicarbonate ion solution |
US20100224503A1 (en) * | 2009-03-05 | 2010-09-09 | Kirk Donald W | Low-energy electrochemical hydroxide system and method |
FI122399B (en) | 2009-06-12 | 2011-12-30 | Nordkalk Oy Ab | Process for the preparation of calcium carbonate |
US20110147227A1 (en) * | 2009-07-15 | 2011-06-23 | Gilliam Ryan J | Acid separation by acid retardation on an ion exchange resin in an electrochemical system |
WO2011066293A1 (en) * | 2009-11-30 | 2011-06-03 | Calera Corporation | Alkaline production using a gas diffusion anode with a hydrostatic pressure |
CN104204351B (en) | 2012-03-23 | 2019-03-12 | 欧米亚国际集团 | The method for being used to prepare scalenohedron winnofil |
WO2013165600A1 (en) * | 2012-05-03 | 2013-11-07 | Calera Corporation | Non-cementitious compositions comprising vaterite and methods thereof |
RU2532189C1 (en) * | 2013-04-22 | 2014-10-27 | Федеральное Государственное Унитарное Предприятие "Государственный Ордена Трудового Красного Знамени Научно-Исследовательский Институт Химических Реактивов И Особо Чистых Химических Веществ" | Method of producing pure calcium carbonate |
CN105377575B (en) | 2013-04-26 | 2017-12-08 | 太平洋纳米产品公司 | Fibre structure amorphous silica including winnofil, the composition of matter being produced from it and its application method |
US9902652B2 (en) | 2014-04-23 | 2018-02-27 | Calera Corporation | Methods and systems for utilizing carbide lime or slag |
CN104804473A (en) * | 2015-04-30 | 2015-07-29 | 建德市双超钙业有限公司 | Production method of special nano calcium carbonate for dual-component high-extrudability building silicone adhesive |
EP3098202A1 (en) | 2015-05-28 | 2016-11-30 | Omya International AG | Process for increasing opacity of precipitated calcium carbonate |
SI3252229T1 (en) | 2016-05-31 | 2019-11-29 | Koehler Se August Papierfabrik | Paper containing scalenoedric precipitated calcium carbonate (s pcc) |
EP3252010A1 (en) | 2016-05-31 | 2017-12-06 | HF Biotec Berlin GmbH | Precipitated calcium carbonate (pcc) with defined grain size and grain size distribution and method for the production thereof |
CN106149434B (en) * | 2016-06-30 | 2018-01-23 | 福建省晋江优兰发纸业有限公司 | A kind of grinding method of high beating degree copy paper |
GB201818580D0 (en) * | 2018-11-14 | 2018-12-26 | Carbon Capture Machine Uk Ltd | Additive for blended cement compositions, cement produced therefrom and method of cement manufacture |
KR20220149530A (en) | 2020-02-25 | 2022-11-08 | 아렐락, 인크. | Method and system for processing lime to form vaterite |
KR20230030619A (en) | 2020-06-30 | 2023-03-06 | 아렐락, 인크. | Methods and systems for forming vaterite from calcined limestone using an electric kiln |
Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3833464A (en) * | 1973-02-16 | 1974-09-03 | Owens Illinois Inc | Method of decolorizing paper mill effluent liquid |
Family Cites Families (83)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US601007A (en) | 1898-03-22 | sturcke | ||
US2211908A (en) | 1937-11-18 | 1940-08-20 | Mead Corp | Manufacture of caustic soda and calcium carbonate |
US2386389A (en) | 1939-06-06 | 1945-10-09 | Chesny | Production of calcium and magnesium compounds from dolomite |
US2462277A (en) | 1946-11-27 | 1949-02-22 | John J Naugle | Method of preparing an activated magnesium oxide |
US2802719A (en) | 1954-05-07 | 1957-08-13 | Souren Z Avedikian | Process of preparing completely carbonated lime |
US3150926A (en) | 1961-05-15 | 1964-09-29 | Champion Papers Inc | Fluidized production of calcium carbonate |
US3304154A (en) | 1964-02-17 | 1967-02-14 | Kiouzes-Pezas Dimitrios | Process for producing spheroidal alkaline earth metal carbonates |
DE2332294C3 (en) | 1973-06-25 | 1980-01-31 | Feldmuehle Ag, 4000 Duesseldorf | Lightweight, high-stiffness, high-volume paper |
US3920800A (en) | 1973-10-12 | 1975-11-18 | Cyprus Mines Corp | Production of purified calcium carbonate |
US4237147A (en) | 1974-01-04 | 1980-12-02 | Monsanto Company | Stabilized amorphous calcium carbonate |
GB1545789A (en) * | 1975-06-04 | 1979-05-16 | Ici Ltd | Manufacture of calcium carbonate magnesium bicarbonate magnesium carbonate and calcium sulphate |
US4157379A (en) | 1976-04-16 | 1979-06-05 | Toyo Soda Manufacturing Co., Ltd. | Process for producing chain structured corpuscular calcium carbonate |
JPS5390199A (en) | 1977-01-20 | 1978-08-08 | Shiraishi Kogyo Kaisha Ltd | Method of modifying calcium carbonate |
LU77723A1 (en) | 1977-07-11 | 1979-03-26 | Solvay | PROCESS FOR THE PREPARATION OF CONCENTRATED AQUEOUS SUSPENSIONS OF CALCIUM CARBONATE |
GB1597190A (en) | 1977-09-19 | 1981-09-03 | Shiraishi Kogyo Kaisha Ltd | Calcium carbonate compositions |
DE2808425A1 (en) | 1978-02-27 | 1979-08-30 | Pluss Stauffer Ag | MINERAL FILLER |
US4244933A (en) | 1978-04-05 | 1981-01-13 | Shiraishi Kogyo Kaisha, Ltd. | Calcium carbonate particles and processes for preparing same |
US4272498A (en) | 1979-09-25 | 1981-06-09 | Foster Wheeler Energy Corporation | Process for comminuting and activating limestone by reaction with CO2 |
US4367207A (en) | 1980-12-18 | 1983-01-04 | Pfizer Inc. | Process for the preparation of finely divided precipitated calcium carbonate |
GB8305346D0 (en) | 1983-02-25 | 1983-03-30 | Ciba Geigy Ag | Particulate calcium carbonate |
US4698219A (en) * | 1983-10-11 | 1987-10-06 | Lummus Crest, Inc. | Treatment of waste from iron ore reduction |
JPS6086067A (en) | 1983-10-18 | 1985-05-15 | 奥多摩工業株式会社 | Manufacture of plate-like calcium hydroxide |
DE3587060T2 (en) | 1984-10-18 | 1993-05-19 | Pfizer | SPHERICAL FILLED CALCIUM CARBONATE, ITS PRODUCTION AND USE. |
US4760138A (en) | 1984-12-13 | 1988-07-26 | Nestec S. A. | Carbonating agents and their preparation |
JPS62113798A (en) | 1985-11-12 | 1987-05-25 | Shinichi Hirano | Production of calcium carbonate single crystal |
US4961823A (en) | 1985-11-12 | 1990-10-09 | Shinichi Hirano | Method of manufacturing calcium carbonate single crystal |
FI73755C (en) | 1985-11-22 | 1987-11-09 | Ekono Oy | FOERFARANDE FOER KAUSTICERING AV EN ALKALIKARBONATHALTIG VATTENLOESNING. |
DE3617169C2 (en) | 1986-05-22 | 1996-05-23 | Pluss Stauffer Ag | Carbonate-containing mineral fillers and pigments |
US4828620A (en) | 1987-08-27 | 1989-05-09 | Southwest Research Institute | Calcination of calcium carbonate and blend therefor |
US4980395A (en) | 1987-11-19 | 1990-12-25 | Pfizer Inc. | Process for the preparation of large surface area, finely divided precipitated calcium carbonate and filled polymeric compositions of matter containing said calcium carbonate |
US4927618A (en) | 1987-11-19 | 1990-05-22 | Pfizer Inc. | Process for the preparation of large surface area, finely divided precipitated calcium carbonate and filled polymeric compositions of matter containing said calcium carbonate |
ATE111142T1 (en) | 1988-03-07 | 1994-09-15 | Pluss Stauffer Ag | PIGMENT MIX FOR THE PAPER INDUSTRY. |
US4824654A (en) | 1988-03-17 | 1989-04-25 | Yabashi Industries Co., Ltd. | Process of producing needle-shaped calcium carbonate particles |
US4892590A (en) | 1988-06-03 | 1990-01-09 | Pfizer Inc. | Precipitated calcium carbonate-cationic starch binder as retention aid system for papermaking |
JP2684112B2 (en) | 1989-06-29 | 1997-12-03 | 丸尾カルシウム株式会社 | Method for producing needle-like aragonite crystalline calcium carbonate |
EP0429707B1 (en) * | 1989-11-29 | 1996-03-27 | SCHAEFER KALK Kommanditgesellschaft | Process for the preparation of basic calcium carbonate, basic calcium carbonate therefrom and its use |
US5156719A (en) | 1990-03-09 | 1992-10-20 | Pfizer Inc. | Acid-stabilized calcium carbonate, process for its production and method for its use in the manufacture of acidic paper |
US5043017A (en) | 1990-03-09 | 1991-08-27 | Pfizer Inc. | Acid-stabilized calcium carbonate, process for its production and method for its use in the manufacture of acidic paper |
US5227025A (en) | 1990-03-13 | 1993-07-13 | Pfizer Inc | Rhombohedral calcium carbonate and accelerated heat-aging process for the production thereof |
US5269818A (en) | 1990-03-13 | 1993-12-14 | Pfizer Inc | Rhombohedral calcium carbonate and accelerated heat-aging process for the production thereof |
US5169682A (en) | 1990-03-28 | 1992-12-08 | Coral Biotech Co., Ltd. | Method of providing silver on calcium carbonate material such as coral sand |
US5059407A (en) | 1990-03-28 | 1991-10-22 | Liquid Carbonic Corporation | Liquid carbon dioxide injection in exothermic chemical reactions |
EP0459399B1 (en) | 1990-05-28 | 1994-08-17 | Maruo Calcium Company Limited | Monodisperse vaterite type calcium carbonate, its manufacturing method and method of controlling growth of particles and shape thereof |
US5223239A (en) | 1990-07-24 | 1993-06-29 | Research Corporation Technologies, Inc. | Method of preparing hydrated lime |
US5558850A (en) | 1990-07-27 | 1996-09-24 | Ecc International Limited | Precipitated calcium carbonate |
GB2246344A (en) | 1990-07-27 | 1992-01-29 | Ecc Int Ltd | Precipitated calcium carbonate |
US5342600A (en) | 1990-09-27 | 1994-08-30 | Ecc International Limited | Precipitated calcium carbonate |
JP2834341B2 (en) | 1990-09-28 | 1998-12-09 | マリーンバイオ株式会社 | Method for producing sintered calcium carbonate and sintered calcium carbonate |
US5164006A (en) | 1991-04-08 | 1992-11-17 | Ecc America Inc. | Method for preparing acid resistant calcium carbonate pigments |
WO1992021613A1 (en) | 1991-06-04 | 1992-12-10 | Minerals Technologies, Inc. | Precipitated calcium carbonate particles from basic calcium carbonate |
US5230734A (en) | 1991-07-29 | 1993-07-27 | Okutama Kogyo Co., Ltd. | Calcium-magnesium carbonate composite and method for the preparation thereof |
DE4128570A1 (en) | 1991-08-28 | 1993-03-04 | Pluss Stauffer Ag | CARBONATE-CONTAINING MINERAL FUELS AND PIGMENTS |
CA2090088C (en) | 1992-02-26 | 1995-07-25 | Pierre Marc Fouche | Production of purified calcium carbonate |
DE4207883A1 (en) | 1992-03-12 | 1993-09-16 | Hoechst Ag | METHOD FOR STABILIZING ETHANOLIC ETHYL MAGNESIUM CARBONATE SOLUTIONS |
WO1993020010A1 (en) | 1992-04-03 | 1993-10-14 | Minerals Technologies, Inc. | Clustered precipitated calcium carbonate particles |
FR2689530B1 (en) | 1992-04-07 | 1996-12-13 | Aussedat Rey | NEW COMPLEX PRODUCT BASED ON FIBERS AND FILLERS, AND METHOD FOR MANUFACTURING SUCH A NEW PRODUCT. |
US5332564A (en) | 1992-07-10 | 1994-07-26 | Ecc International Inc. | Process for production of rhombic shaped precipitated calcium carbonate |
US5330760A (en) | 1992-08-27 | 1994-07-19 | Sterling Winthrop Inc. | Effervescent antacid |
US5364828A (en) | 1992-10-21 | 1994-11-15 | Minerals Technologies | Spheroidal aggregate of platy synthetic hydrotalcite |
US5364610A (en) | 1993-06-15 | 1994-11-15 | P. H. Glatfelter Company | Process for preparation of high opacity precipitated calcium carbonate by reacting sodium carbonate with calcium hydroxide |
US5411639A (en) | 1993-10-15 | 1995-05-02 | Westvaco Corporation | Process for enhancing sizing efficiency in filled papers |
US5455050A (en) | 1993-11-12 | 1995-10-03 | Mcneil-Ppc, Inc. | Aqueous antacids with calcium carbonate and magnesium salt |
ES2113056T3 (en) | 1993-12-14 | 1998-04-16 | Ecc Int Ltd | RECOVERY OF WATER AND SOLIDS IN A PAPER FACTORY. |
US5413635A (en) | 1993-12-30 | 1995-05-09 | Fuller Company | Lime sludge treatment process |
DK172100B1 (en) | 1994-03-22 | 1997-10-27 | Smidth & Co As F L | Process for heat treatment of lime sludge, as well as systems for carrying out the process |
US5505819A (en) | 1994-03-31 | 1996-04-09 | Macmillan Bloedel Limited | Neutral papermaking |
US5500131A (en) | 1994-04-05 | 1996-03-19 | Metz; Jean-Paul | Compositions and methods for water treatment |
DE4416895C1 (en) | 1994-05-13 | 1995-10-19 | Pluss Stauffer Ag | Carbonate-containing mineral fillers and their use as matting agents |
US5690897A (en) | 1994-11-21 | 1997-11-25 | Minerals Technologies Inc. | Method for purification of calcium carbonate |
AU3795395A (en) | 1994-11-30 | 1996-06-06 | Ethicon Inc. | Hard tissue bone cements and substitutes |
US5665205A (en) | 1995-01-19 | 1997-09-09 | International Paper Company | Method for improving brightness and cleanliness of secondary fibers for paper and paperboard manufacture |
US5759258A (en) | 1995-03-15 | 1998-06-02 | Minerals Technologies Inc. | Recycling of mineral fillers from the residue of a paper deinking plant |
US5643631A (en) | 1995-03-17 | 1997-07-01 | Minerals Tech Inc | Ink jet recording paper incorporating novel precipitated calcium carbonate pigment |
US5676747A (en) | 1995-12-29 | 1997-10-14 | Columbia River Carbonates | Calcium carbonate pigments for coating paper and paper board |
US5653795A (en) | 1995-11-16 | 1997-08-05 | Columbia River Carbonates | Bulking and opacifying fillers for cellulosic products |
US5595819A (en) | 1995-04-21 | 1997-01-21 | E. I. Du Pont De Nemours And Company | Thin polyester film containing cubic calcium carbonate particles suitable for capacitor, digital stencil and thermal transfer media |
US5518540A (en) | 1995-06-07 | 1996-05-21 | Materials Technology, Limited | Cement treated with high-pressure CO2 |
US5531821A (en) | 1995-08-24 | 1996-07-02 | Ecc International Inc. | Surface modified calcium carbonate composition and uses therefor |
US5599388A (en) | 1995-08-24 | 1997-02-04 | Ecc International Inc. | Acid resistant calcium carbonate composition containing an aluminum salt, uses therefor and processes for its production |
US5593488A (en) | 1995-08-24 | 1997-01-14 | Ecc International Inc. | Acid resistant calcium carbonate composition and uses therefor |
DK0851839T3 (en) | 1995-09-20 | 2002-07-29 | Chemical Lime Ltd | Process for producing high purity calcium carbonate |
GB9520703D0 (en) | 1995-10-10 | 1995-12-13 | Ecc Int Ltd | Paper coating pigments and their production and use |
US5593489A (en) | 1995-10-20 | 1997-01-14 | Ecc International Inc. | Acid resistant carbonate composition containing an aluminum or magnesium hydroxide methods of preparation and uses therefor |
-
1999
- 1999-07-21 US US09/358,759 patent/US6251356B1/en not_active Expired - Lifetime
-
2000
- 2000-07-21 CA CA002416080A patent/CA2416080C/en not_active Expired - Lifetime
- 2000-07-21 EP EP00950496A patent/EP1230160A4/en not_active Withdrawn
- 2000-07-21 AU AU63595/00A patent/AU6359500A/en not_active Abandoned
- 2000-07-21 WO PCT/US2000/019867 patent/WO2001007365A1/en active Application Filing
-
2001
- 2001-02-22 US US09/791,433 patent/US20020009410A1/en not_active Abandoned
Patent Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3833464A (en) * | 1973-02-16 | 1974-09-03 | Owens Illinois Inc | Method of decolorizing paper mill effluent liquid |
Cited By (41)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN100389068C (en) * | 2004-09-24 | 2008-05-21 | 曲玉珠 | Preparation of light calcium carbonate by calcite |
US8857118B2 (en) | 2007-05-24 | 2014-10-14 | Calera Corporation | Hydraulic cements comprising carbonate compound compositions |
US7735274B2 (en) | 2007-05-24 | 2010-06-15 | Calera Corporation | Hydraulic cements comprising carbonate compound compositions |
US7906028B2 (en) | 2007-05-24 | 2011-03-15 | Calera Corporation | Hydraulic cements comprising carbonate compound compositions |
US7744761B2 (en) | 2007-06-28 | 2010-06-29 | Calera Corporation | Desalination methods and systems that include carbonate compound precipitation |
US7931809B2 (en) | 2007-06-28 | 2011-04-26 | Calera Corporation | Desalination methods and systems that include carbonate compound precipitation |
US7914685B2 (en) | 2007-06-28 | 2011-03-29 | Calera Corporation | Rocks and aggregate, and methods of making and using the same |
US7753618B2 (en) | 2007-06-28 | 2010-07-13 | Calera Corporation | Rocks and aggregate, and methods of making and using the same |
US7887694B2 (en) | 2007-12-28 | 2011-02-15 | Calera Corporation | Methods of sequestering CO2 |
US8333944B2 (en) | 2007-12-28 | 2012-12-18 | Calera Corporation | Methods of sequestering CO2 |
US7754169B2 (en) | 2007-12-28 | 2010-07-13 | Calera Corporation | Methods and systems for utilizing waste sources of metal oxides |
US7749476B2 (en) | 2007-12-28 | 2010-07-06 | Calera Corporation | Production of carbonate-containing compositions from material comprising metal silicates |
US9260314B2 (en) | 2007-12-28 | 2016-02-16 | Calera Corporation | Methods and systems for utilizing waste sources of metal oxides |
EP2268863B1 (en) | 2008-03-07 | 2019-12-18 | FP-Pigments Oy | A pigment particle composition, its method of manufacture and its use |
US8894830B2 (en) | 2008-07-16 | 2014-11-25 | Celera Corporation | CO2 utilization in electrochemical systems |
US7875163B2 (en) | 2008-07-16 | 2011-01-25 | Calera Corporation | Low energy 4-cell electrochemical system with carbon dioxide gas |
US7993500B2 (en) | 2008-07-16 | 2011-08-09 | Calera Corporation | Gas diffusion anode and CO2 cathode electrolyte system |
US8357270B2 (en) | 2008-07-16 | 2013-01-22 | Calera Corporation | CO2 utilization in electrochemical systems |
US9017631B2 (en) | 2008-08-13 | 2015-04-28 | Omya International Ag | Process to prepare precipitated calcium carbonate implementing low charge acrylate a/o maleinate-containing polymer |
EP2157136A1 (en) | 2008-08-13 | 2010-02-24 | Omya Development Ag | Process to prepare precipitated calcium carbonate implementing low charge acrylate a/o maleinate-containing polymer |
US7966250B2 (en) | 2008-09-11 | 2011-06-21 | Calera Corporation | CO2 commodity trading system and method |
US8006446B2 (en) | 2008-09-30 | 2011-08-30 | Calera Corporation | CO2-sequestering formed building materials |
US7939336B2 (en) | 2008-09-30 | 2011-05-10 | Calera Corporation | Compositions and methods using substances containing carbon |
US7815880B2 (en) | 2008-09-30 | 2010-10-19 | Calera Corporation | Reduced-carbon footprint concrete compositions |
US7771684B2 (en) | 2008-09-30 | 2010-08-10 | Calera Corporation | CO2-sequestering formed building materials |
US8431100B2 (en) | 2008-09-30 | 2013-04-30 | Calera Corporation | CO2-sequestering formed building materials |
US8470275B2 (en) | 2008-09-30 | 2013-06-25 | Calera Corporation | Reduced-carbon footprint concrete compositions |
US8869477B2 (en) | 2008-09-30 | 2014-10-28 | Calera Corporation | Formed building materials |
US8603424B2 (en) | 2008-09-30 | 2013-12-10 | Calera Corporation | CO2-sequestering formed building materials |
US7829053B2 (en) | 2008-10-31 | 2010-11-09 | Calera Corporation | Non-cementitious compositions comprising CO2 sequestering additives |
US9133581B2 (en) | 2008-10-31 | 2015-09-15 | Calera Corporation | Non-cementitious compositions comprising vaterite and methods thereof |
US7790012B2 (en) | 2008-12-23 | 2010-09-07 | Calera Corporation | Low energy electrochemical hydroxide system and method |
US8834688B2 (en) | 2009-02-10 | 2014-09-16 | Calera Corporation | Low-voltage alkaline production using hydrogen and electrocatalytic electrodes |
US9267211B2 (en) | 2009-02-10 | 2016-02-23 | Calera Corporation | Low-voltage alkaline production using hydrogen and electrocatalytic electrodes |
US8491858B2 (en) | 2009-03-02 | 2013-07-23 | Calera Corporation | Gas stream multi-pollutants control systems and methods |
US8883104B2 (en) | 2009-03-02 | 2014-11-11 | Calera Corporation | Gas stream multi-pollutants control systems and methods |
US8137444B2 (en) | 2009-03-10 | 2012-03-20 | Calera Corporation | Systems and methods for processing CO2 |
US7993511B2 (en) | 2009-07-15 | 2011-08-09 | Calera Corporation | Electrochemical production of an alkaline solution using CO2 |
CN102423608A (en) * | 2011-10-28 | 2012-04-25 | 长沙理工大学 | Desulfurizer prepared by causticized white mud and method thereof for flue gas desulphurization |
WO2014016469A1 (en) * | 2012-07-27 | 2014-01-30 | Upm-Kymmene Corporation | A method and a system for preventing calender blackening |
RU2533143C1 (en) * | 2013-03-26 | 2014-11-20 | Геннадий Георгиевич Волокитин | Method of obtaining ultradispersive powders of carbonates |
Also Published As
Publication number | Publication date |
---|---|
CA2416080C (en) | 2009-05-26 |
US20020009410A1 (en) | 2002-01-24 |
EP1230160A4 (en) | 2003-07-16 |
AU6359500A (en) | 2001-02-13 |
WO2001007365A9 (en) | 2002-07-25 |
US6251356B1 (en) | 2001-06-26 |
EP1230160A1 (en) | 2002-08-14 |
CA2416080A1 (en) | 2001-02-01 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US6251356B1 (en) | High speed manufacturing process for precipitated calcium carbonate employing sequential perssure carbonation | |
US7048900B2 (en) | Method and apparatus for production of precipitated calcium carbonate and silicate compounds in common process equipment | |
JP2939659B2 (en) | Precipitated calcium carbonate | |
CA2290816C (en) | Seeding of aragonite calcium carbonate and the product thereof | |
US11111388B2 (en) | Precipitated calcium carbonate with improved resistance to structural breakdown | |
MX2011005665A (en) | Process for manufacturing calcium carbonate materials having a particle surface with improved adsorption properties. | |
JPH07509684A (en) | Clustered precipitated calcium carbonate particles | |
EP0522068B1 (en) | Liquid carbon dioxide injection in exothermic chemical reactions | |
CN101326123A (en) | Particles of precipitated calcium carbonate, process for making the particles and use of the particles as filler | |
US20220106194A1 (en) | Process for producing nano precipitated calcium carbonate | |
US20060099132A1 (en) | Process for the production of precipitated calcium carbonates and product produced thereby | |
JP3874449B2 (en) | Method for producing light calcium carbonate | |
EP0772570B1 (en) | Magnesium hydroxide slurries | |
JP4157202B2 (en) | Process for producing spindle-shaped calcium carbonate | |
WO2005044728A2 (en) | Methods and apparatus for producing precipitated calcium carbonate | |
JP2002234726A (en) | Continuous producing method of calcium carbonate | |
JPH01301510A (en) | Production of fusiform calcium carbonate | |
CN116528963A (en) | Method for producing calcium carbonate and calcium carbonate | |
JPS62113718A (en) | Production of hexagonal complex of calcium carbonate | |
JPH05270821A (en) | Production of cubic calcium carbonate | |
KR19980051472A (en) | Method for producing cubic calcium carbonate |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AK | Designated states |
Kind code of ref document: A1 Designated state(s): AE AL AM AT AU AZ BA BB BG BR BY CA CH CN CR CU CZ DE DK DM EE ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX NO NZ PL PT RO RU SD SE SG SI SK SL TJ TM TR TT TZ UA UG US UZ VN YU ZA ZW |
|
AL | Designated countries for regional patents |
Kind code of ref document: A1 Designated state(s): GH GM KE LS MW MZ SD SL SZ TZ UG ZW AM AZ BY KG KZ MD RU TJ TM AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE BF BJ CF CG CI CM GA GN GW ML MR NE SN TD TG |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application | ||
DFPE | Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101) | ||
WWE | Wipo information: entry into national phase |
Ref document number: IN/PCT/2002/00054/DE Country of ref document: IN |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2000950496 Country of ref document: EP |
|
REG | Reference to national code |
Ref country code: DE Ref legal event code: 8642 |
|
AK | Designated states |
Kind code of ref document: C2 Designated state(s): AE AL AM AT AU AZ BA BB BG BR BY CA CH CN CR CU CZ DE DK DM EE ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX NO NZ PL PT RO RU SD SE SG SI SK SL TJ TM TR TT TZ UA UG US UZ VN YU ZA ZW |
|
AL | Designated countries for regional patents |
Kind code of ref document: C2 Designated state(s): GH GM KE LS MW MZ SD SL SZ TZ UG ZW AM AZ BY KG KZ MD RU TJ TM AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE BF BJ CF CG CI CM GA GN GW ML MR NE SN TD TG |
|
COP | Corrected version of pamphlet |
Free format text: PAGES 1/27-27/27, DRAWINGS, REPLACED BY NEW PAGES 1/25-25/25; DUE TO LATE TRANSMITTAL BY THE RECEIVING OFFICE |
|
WWP | Wipo information: published in national office |
Ref document number: 2000950496 Country of ref document: EP |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2416080 Country of ref document: CA |
|
NENP | Non-entry into the national phase |
Ref country code: JP |